|Publication number||US7470350 B2|
|Application number||US 11/737,788|
|Publication date||Dec 30, 2008|
|Filing date||Apr 20, 2007|
|Priority date||Apr 25, 2006|
|Also published as||US20070246344|
|Publication number||11737788, 737788, US 7470350 B2, US 7470350B2, US-B2-7470350, US7470350 B2, US7470350B2|
|Inventors||Ian Richard Bonnett, Anthony Busigin|
|Original Assignee||Ge Healthcare Uk Limited|
|Export Citation||BiBTeX, EndNote, RefMan|
|Patent Citations (8), Non-Patent Citations (13), Referenced by (10), Classifications (21), Legal Events (3)|
|External Links: USPTO, USPTO Assignment, Espacenet|
This invention claims priority to U.S. provisional patent application No. 60/745,554 filed Apr. 25, 2006; the disclosure of which is incorporated herein by reference in its entirety.
This invention relates generally to the field of tritium isotope recovery from water and more specifically to a process for tritium removal from light water by water distillation stripping and enrichment, followed by conversion of tritium enriched water to an elemental hydrogen stream, and final tritium enrichment by thermal diffusion.
Several large scale facilities have been built in Canada, France, and more recently South Korea, to extract tritium from heavy water moderator systems for nuclear reactors. Kalyanam and Sood, “Fusion Technology” 1988, pp 525-528, provide a comparison of the process characteristics of these types of systems. Similar although smaller light water tritium recovery systems have been designed for fusion applications (see H. Yoshida, et al, “Fusion Eng. and Design” 1998, pp 825-882; Busigin et al, “Fusion Technology”, 1995 pp 1312-1316; A. Busigin and S. K. Sood, “Fusion Technology” 1995 pp 544-549). All current large scale tritium recovery systems employ a front-end process to transfer tritium from water to elemental hydrogen, followed by a cryogenic distillation cascade to perform all or most of the hydrogen isotope separation.
Thermal diffusion columns have been used to separate hydrogen isotopes on a small scale since the 1950's as described by G. Vasaru et al, “The Thermal Diffusion Column”, VEB Deutscher der Wissenschaften, Berlin, 1968.The use of this technology has been limited because it is not scaleable to large throughputs.
All commercial large scale processes for water detritiation are based on transfer of tritium from water to elemental hydrogen by: (a) a catalytic exchange reaction such as HTO+H2→H2O+HT; (b) direct electrolysis of water, i.e., HTO→HT+½O2; or (c) water decomposition by a suitable reaction such as the water gas shift reaction: HTO+CO→HT+CO2. (See Kalyanam and Sood “Fusion Technology” 1988, pp 525-528; A. Busigin and P. Gierszewski, “Fusion Engineering and Design” 1998 pp 909-914; D. K. Murdoch et al, “Fusion Science and Technology” 2005, pp 3-10; K. L. Sessions, “Fusion Science and Technology” 2005, pp 91-96; J. Cristescu et al, “Fusion Science and Technology” 2005, pp 97-101; J. Cristescu et al, “Fusion Science and Technology” 2005, pp 343-348.)
The prior art large scale hydrogen isotope separation cryogenic distillation process has the following drawbacks:
Water distillation has been used in the past primarily for heavy water production and upgrading, and not specifically for tritium recovery. Tritium is easier to separate than deuterium from light water by water distillation. The elementary separation factors in distillation arise from differences in vapor pressures of the isotopic water species. For example, at a temperature of 51° C., the elementary separation factor for HDO/H2O is 1.052, whereas for HTO/H2O it is 1.064.The separation factor for DTO/D2O is much smaller at 1.012, making tritium recovery from heavy water by water distillation difficult. (W. Alexander Van Hook, Journal of Physical Chemistry, Vol. 72, No. 4, pp 1234-1244, 1968.)
Due to presence of natural deuterium at approximately 150 ppm, water distillation enrichment of tritium in light water is easy only when the deuterium concentration is small, which corresponds to a maximum practical enrichment in light water of about 1000 times. This degree of tritium enrichment is sufficient in many practical applications to reduce the tritium enriched product flow to a magnitude compatible with one or more downstream thermal diffusion columns, after conversion of water to an elemental hydrogen stream.
Thermal diffusion has been used successfully for small scale tritium separation, even up to ≧99% tritium, but cannot be easily scaled for large throughput. This is because thermal diffusion columns must operate in the laminar flow regime, and scale-up would push column operation into the turbulent flow regime (R. Clark Jones and W. H. Furry, “Reviews of Modern Physics”, 1946, pp 151-224). The alternative of constructing many small thermal diffusion columns in parallel is unattractive when the throughput requirement is large. Thermal diffusion columns also have low thermodynamic efficiency, which while unimportant at small scale becomes problematic at large scale.
In a first aspect of the invention, there is provided a process for recovery of tritium from a mixture containing heavy and light hydrogen isotopes in a water feed material, which process comprises:
According to a preferred embodiment of the invention, there is provided a process for tritium removal from a mixture containing heavy and light water by water distillation tritium stripping and enrichment, followed by conversion of tritiated water to an elemental hydrogen stream, followed by final tritium enrichment by thermal diffusion. When combined with a suitable oxidation process, the method therefore provides a multi-stage procedure for converting complex tritium-labelled organic and/or inorganic waste products, which may arise from laboratory and other industrial processes, into a simple elemental form of tritium. In the context of the present invention, the term “heavy” isotopes in a water feed material is intended to mean water containing the tritium isotope of hydrogen. Correspondingly, the term “light” isotopes in a water feed material is intended to mean water containing protium (and small amounts of deuterium) isotope of hydrogen. Suitably, the process is capable of de-tritiating water containing parts per million of tritium and generating tritium at at least 90% isotopic abundance, and preferably at least 99% isotopic abundance. This process benefits from the effectiveness of tritium stripping and enrichment by water distillation of light water at large throughputs and low tritium concentrations with the simplicity of thermal diffusion for the small throughput required for final enrichment. Furthermore, the process may be adjusted to provide a large-scale non-cryogenic process for de-tritiation of light water that is simpler and more economical than a conventional cryogenic distillation process. Such a process is simpler to start-up, shutdown, operate and provides a process having reduced hazards through elimination of liquid cryogens, by comparison with a conventional cryogenic distillation process. Furthermore, the process requires a significantly smaller elemental hydrogen isotope inventory than a conventional cryogenic distillation process.
Suitably, the process may be operated batchwise, or alternatively in a continuous process. Preferably, the process is a continuous process. Thus, the process is compatible with any intermediate conversion process to convert tritiated water to elemental hydrogen including electrolysis, water decomposition by water gas shift reactor (i.e. palladium membrane reactor) or a hot metal bed reactor.
The drawings constitute a part of this specification and include exemplary embodiments to the invention, which may be embodied in various forms. It is to be understood that in some instances various aspects of the invention may be shown exaggerated or enlarged to facilitate an understanding of the invention.
Detailed descriptions of the preferred embodiment of the present invention are provided herein. It is to be understood, however, that the present invention may be embodied in various forms. Therefore, specific details disclosed herein are not to be interpreted as limiting, but rather as a basis for the claims and as a representative basis for teaching one skilled in the art to employ the present invention in virtually any appropriately detailed system, structure or manner.
In accordance with one embodiment of the present invention,
In one embodiment, each column is filled with a packing material employed to improve interfacial liquid to vapor contact and therefore to increase separation efficiency of the tritium/hydrogen containing water mixture. In principle, any suitable packing material may be used, providing that such material is inert under the distillation conditions employed. Examples include glass beads, phosphor bronze metal beads, perforated metal strips and the like. Alternatively, a structured packing such as Sulzer BX or CY. For optimum separation, preferably each column is packed with mesh rings each formed into a cylindrical shape and being fabricated from stainless steel (Dixon rings). Dixon rings vary from 1.5 mm to 6.0 mm in diameter, and can provide a large surface area in a small volume, thereby enabling efficient separation.
In one embodiment, each of the water distillation columns may be fitted with one or more, preferably up to six liquid distributors at intervals inside the column. Fitting of such liquid distributors enables a randomly packed column to overcome the tendency of liquid in such columns to migrate towards the walls of the column which may reduce contact between liquid and vapor, and as a consequence may reduce column efficiency. There are many known designs of liquid distributor, see for example “Liquid Distribution for Optimum Packing Performance”, D Perry, D E Nutter and A Hale, Chem.Eng.Progress, (1990) p 30-35. Known liquid distributors do not function efficiently at low flow rates. A preferred liquid distributor is one which operates efficiently at low water flow rates and is shown in
Referring again to
In a second conversion stage of the process, water enriched in heavier hydrogen from step i) is converted into a mixture of hydrogen isotopes. The conversion process may suitably be performed by an electrolysis cell, a water-gas shift reactor or other conversion process. A suitable process for the recovery of hydrogen and hydrogen isotopes from water is described in U.S. Pat. No. 6,165,438 (Willms et al.). Feed material from step i) of the process is mixed with carbon monoxide (in the presence of carrier Argon gas) and converted under catalytic conditions into a mixture of hydrogen isotopes and oxides of carbon. The inlet gas mixture is caused to flow over a heated catalyst which promotes the following reaction: H2O+CO→H2+CO2 (Water-gas shift reaction). The preferred palladium membrane reactor design is shown schematically (
In operation, reactants consisting of a mixture of tritiated water (from the distillation process of step i), carbon monoxide and argon are fed into the conversion apparatus and passed through the heated palladium membrane tube, thereby promoting the water-gas shift reaction. The reactor temperature is suitably between about 450° C. and about 550° C. In a preferred embodiment, the reactor temperature is held at 475° C.
During the time that the reaction takes place in the presence of the heated catalyst, hydrogen and tritium are extracted through the palladium/silver membrane by pumping annular space within the vacuum tight shell (26) to high vacuum. The permeate, thus enriched in hydrogen and tritium, is then passed to the final stage (step iii)) of the process. The mixture of gases which do not pass through the palladium/silver (termed the retentate (23) and consisting of a mixture of carbon dioxide and argon) is monitored and may be discharged to waste.
In step iii) of the process, the elemental hydrogen stream (22) is fed to the thermal diffusion column (30) for final enrichment of tritium. The thermal diffusion column is shown in
By combining the scalability of the water distillation column (10) with one or more small throughput thermal diffusion columns (30), the overall process makes optimal use of water distillation and thermal diffusion. Either process option on its own is either unattractive or impractical. Furthermore, the combined water distillation and thermal diffusion system is much simpler to operate than a conventional cryogenic distillation cascade. There are no complex startup, operation, or shutdown sequences. The process may be employed in continuous mode with no necessity for batch operations.
The present invention also provides a combined water distillation and thermal diffusion process for converting tritiated water to elemental hydrogen and tritium. This process comprises: (i) distilling a sample of water containing a mixture of hydrogen isotopes under conditions to separate water containing lighter hydrogen from water containing heavier hydrogen from the mixture; (ii) converting tritiated water to elemental hydrogen by a process selected from electrolysis and water gas shift reactor; and (iii) separating hydrogen isotopes from step (ii) by thermal diffusion.
The present invention also provides a system for converting tritiated water containing a mixture of hydrogen isotopes into elemental hydrogen and tritium, the system comprising: a) distillation means for distilling a sample of water containing said mixture of hydrogen isotopes; b) conversion means for converting water enriched in heavy hydrogen under catalytic conditions and in the presence of carbon monoxide into a mixture of hydrogen isotopes and oxides of carbon; and c) separation means for separating hydrogen isotopes.
While aspects of the invention has been described in connection with a preferred embodiment, it is not intended to limit the scope of the invention to the particular form set forth, but on the contrary, it is intended to cover such alternatives, modifications, and equivalents as may be included within the spirit and scope of the invention as defined by the appended claims.
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|1||Busigin, et al., "CFTSIM-ITR Dynamic Fuel Cycle Model", Fusion Engineering and Design, 39-40, 1998, pp. 909-914.|
|2||Busigin, et al., "Installation and Early Operation of a Complex Low Inventory Cryogenic Distillation System for the Princeton TFTR", Fusion Technology, Colume 28, 1995 pp. 1312-1316.|
|3||Busigin, et al., "Steady State and Dynamic Simulation of the ITER Hydrogen Isotope Separation System", Fusion Technology, vol. 28, 1995 pp. 544-549.|
|4||Cristescu, et al., "ITER Dynamic Tritium Inventory Modeling Code", Fusion Science and Technology, vol. 48, 2005 pp. 343-348.|
|5||Cristescu, et al., "Trenta Facility for Trade-Off Studies Between Combined Electrolysis Catalytic Exchange and Cryogenic Distillation Processes", Fusion Science and Technology, vol. 48, 2005, pp. 97-101.|
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|9||Perry, et al., "Liquid Distribution for Optimum Packing Performance", Chemical Engineering Progress, 1990, pp. 30-35.|
|10||Sessions, "Processing Tritiated Water at the Savannah River Site: A Production-Scale Demonstration of a Palladium Membrane Reactor", Fusion Science and Technology, vol. 48, 2005, pp. 91-96.|
|11||Van Hook, "Vapor Pressure of the Isotopic Waters and Ices", Journal of Physical Chemistry, vol. 72, No. 4, 1968, pp. 1234-1244.|
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|U.S. Classification||203/5, 423/648.1, 203/12, 202/154, 203/71, 202/158, 423/655, 422/177|
|International Classification||B01D17/09, B01D59/04, B01D59/16, C01B3/50, B01D53/22|
|Cooperative Classification||B01D59/16, C01B4/00, B01D59/04, B01D59/50|
|European Classification||B01D59/50, B01D59/16, C01B4/00, B01D59/04|
|Aug 13, 2012||REMI||Maintenance fee reminder mailed|
|Dec 30, 2012||LAPS||Lapse for failure to pay maintenance fees|
|Feb 19, 2013||FP||Expired due to failure to pay maintenance fee|
Effective date: 20121230